Preparation of aliphatic, alpha omega-aminonitriles

ABSTRACT

Aliphatic alpha,omega-aminonitriles are prepared by partial hydrogenation of aliphatic alpha,omega-dinitriles at elevated temperatures and superatmospheric pressure in the presence of a solvent and of a catalyst by a process in which the catalyst 
     (a) contains a compound based on a metal selected from the group consisting of nickel, cobalt, iron, ruthenium and rhodium and 
     (b) contains from 0.01 to 25% by weight, based on (a), of a promoter based on a metal selected from the group consisting of palladium, platinum, iridium, osmium, copper, silver, gold, chromium, molybdenum, tungsten, manganese, rhenium, zinc, cadmium, lead, aluminum, tin, phosphorus, arsenic, antimony, bismuth and rare earth metals and 
     (c) from 0 to 5% by weight, based on (a), of a compound based on an alkali metal or on an alkaline earth metal, 
     with the proviso that the component (a) is not based on iron or iron and one of the metals selected from the group consisting of cobalt, ruthenium and rhodium when (b) is a promoter based on a metal selected from the group consisting of titanium, manganese, chromium and molybdenum, and with the further proviso that, when a compound based on only ruthenium or ruthenium and rhodium or nickel and rhodium is selected as component (a), the promoter (b) may be dispensed with.

This application is a C-I-P of U.S. Ser. No. 08/375,573 of Jan. 18,1995, now U.S. Pat. No. 5,527,946.

Present invention relates to an improved process for the preparation ofaliphatic alpha,omega-aminonitriles by partial hydrogenation ofaliphatic alpha,omega-dinitriles at elevated temperature andsuperatmospheric pressure in the presence of a solvent and a catalyst.

WO 92/21650 describes the partial hydrogenation of adiponitrile to6-aminocapronitrile in the presence of a Raney nickel catalyst andammonia as a solvent in a yield of 60% at a conversion of 70%.Hexamethylenediamine is formed in the amount of 9% as a byproduct. Thedisadvantage of this process is the short life of the catalyst.

U.S. Pat. No. 2,257,814 and U.S. Pat. No. 2,208,598 likewise describepreparation processes of 6-aminocapronitrile starting from adiponitrile,the catalysts used being Raney cobalt or iron, nickel and cobaltcatalysts on various carriers. The fact that the selectivities of from50 to 60% are too low for industrial applications is a disadvantage ofthese processes.

In the process of WO 93/16034, the yield of aminocapronitrile can beincreased by hydrogenating adiponitrile in the presence of Raney nickel,of a base, such as sodium hydroxide, potassium hydroxide, lithiumhydroxide or ammonium hydroxide, and of a transition metal complexcontaining, for example, iron, cobalt, chromium or tungsten astransition metals, and of a solvent. In this process, quantitativeyields of aminocapronitrile are said to be obtained at conversions offrom 45 to 60%. The disadvantage of this process is the working up ofthe generally toxic transition metal complexes from the reactionmixtures obtained.

EP-A 161,419 describes the partial hydrogenation of adiponitrile using arhodium-containing catalyst on a magnesium oxide carrier. At aconversion of 70%, a selectivity of 94% is achieved. The disadvantage isthe expensive preparation method of the Rh/MgO catalysts (cf. J. of Cat.112 (1988), 145-156).

DE-A 4,235,466 describes the fixed-bed hydrogenation of adiponitrile to6-aminocapronitrile over an iron sponge catalyst (unsupported catalyst)which was prepared from iron ore by a special method and subsequentlydoped with cobalt, titanium, manganese, chromium, molybdenum, rutheniumor iridium. Owing to the small surface area (0.8 m² /g), these catalystsgenerally have useful activity only at high pressures and hightemperatures. A further disadvantage of this process is the rapid lossof activity: in spite of a reduction in the adiponitrile and hydrogenloading, which leads to an increase in conversion, according to Example7 the conversion decreased by 5% in the course of 24 hours.

DE-A 848,654 describes the continuous fixed-bed hydrogenation ofadiponitrile over palladium on silica gel and over metals of the eighthgroup of the Periodic Table, these metals preferably being used in theform of spinels. A substantial disadvantage of these catalysts is theirunsatisfactory life.

It was found that catalysts based on iron with a BET-surface(Brunauer-Emmett Teller) of greater than 5 m² /g and a carbon content ofnot more than 0.4% by weight, based on the total amount of the catalyst,are very useful for the preparation of aliphaticalpha,omega-aminonitriles by partial hydrogenation of aliphaticalpha,omega-dinitriles. Such Fe-catalysts are known and used ascatalysts in the synthesis of ammonia, the Fisher-Tropsch-reaction orthe preparation of styrene from ethyl benzene. The corresponding ironoxide precursors are obtainable from iron oxides such as hematite ormagnetite or by oxidation of iron or starting from iron cyanides,carbides, and nitrides according to Ullmann's Encyclopedia of IndustrialChemistry, 5th Edition, vol. A2, p. 169-172. Promotors may be added bymelting the corresponding oxides or by well-known impregnationtechniques. Iron oxide precursors are also obtainable by precipitationmethods (for example described in B. E. Leach, Applied IndustrialCatalysis, vol. 2, 1983, pp. 177-180) or by coprecipitation on inertoxidic carriers by adding starting from aqueous solutions of iron saltsand with carbonates or hydroxides. The obtained precursors can betransformed into extrudates or pellets as described for example inCatalyst Manufacture, A. B. Stiles (1983), pp. 123-124 and M. Sittig,Catalyst Manufacture, Recovery and Use, 1972, Noyes data corporation,pp. 217-221.

It is an object of the present invention to provide an improved processfor the preparation of aliphatic alpha,omega-aminonit-riles by partialhydrogenation of adiponitrile, which process does not have theabovementioned disadvantages; in particular, it is intended to provide aprocess in which the catalysts used have a longer life than those of theprior art.

We have found that this object is achieved by a process for thepreparation of aliphatic alpha,omega-aminonitriles by partialhydrogenation of aliphatic alpha,omega-dinitriles at elevatedtemperatures and superatmospheric pressure in the presence of a solventand of a catalyst, which comprises using a catalyst which

(a) contains a compound based on a metal selected from the groupconsisting of nickel, cobalt, iron, ruthenium or rhodium and

(b) contains from 0.01 to 25, preferably from 0.1 to 5, % by weight,based on (a), of a promoter based on a metal selected from the groupconsisting of palladium, platinum, iridium, osmium, iron, copper,silver, gold, chromium, molybdenum, tungsten, manganese, rhenium, zinc,cadmium, lead, aluminum, tin, phosphorus, arsenic, antimony, bismuth orrare earth metals and

(c) from 0 to 5% by weight, based on (a), of a trace component based ona metal selected from the group consisting of an alkali metal and analkaline earth metal,

with the proviso that the component (a) is not based on

iron or

iron and one of the metals selected from the group consisting of cobalt,ruthenium and rhodium when (b) is a promoter based on a metal selectedfrom the group consisting of titanium, manganese, chromium andmolybdenum, and with the further proviso that, when a compound based ononly

ruthenium or

rhodium or

ruthenium and rhodium or

rhodium and nickel

is selected as component (a), the promoter (b) may, if desired, bedispensed with, whereby the catalyst is obtained by

(I) impregnating a catalyst carrier with a solution of the components(a), (b) and, if desired, (c), where the individual components may beadded simultaneously or in succession, or by spraying the solutions ofthe components (a), (b) and, if desired, (c) onto the carrier by amethod known per se, then

(II) if desired processing the resulting impregnated carrier to giveextrudates or pellets, then

(III) drying the impregnated carrier, extrudates or pellets at atemperature from 80° to 150° C. yielding a dried product, and

(IV) then calcining the dried product at a temperature from 150° to1000° C. in a gas stream comprising air or nitrogen yielding a calcinedproduct, then

(V) if desired, passivating the surface of the calcined product at from20° to 80° C. by means of an oxygen/nitrogen mixture yielding apassivated product, then

(VI) activating the calcined or passivated product by exposing it to areducing atmosphere for from 2 to 24 hours at from 200° to 500° C.

In another embodiment of the invention, the objective stated above canbe achieved by a process for the preparation of aliphaticalpha,omega-aminonitriles by partial hydrogenation of aliphaticalpha,omega-dinitriles at elevated temperature and superatmosphericpressure in the presence of a solvent and of a catalyst, which comprisescarrying out the partial dehydrogenation in the presence of a catalystwhich

(a) contains a compound based on a metal selected from the groupconsisting of iron, nickel, ruthenium and rhodium and

(b) contains from 0.01 to 25% by weight, based on (a), of a promoterbased on a metal selected from the group consisting of palladium,platinum, iridium, osmium, iron, copper, silver, gold, chromium,molybdenum, tungsten, manganese, rhenium, zinc, cadmium, lead, aluminum,tin, phosphorus, arsenic, antimony, bismuth and rare earth metals, and

(c) from 0 to 5% by weight, based on (a), of a trace component based ona metal selected from the group consisting of an alkali metal and analkaline earth metal,

with the proviso that the component (a) is not based on

iron or

iron and one of the metals selected from the group consisting of cobalt,ruthenium and rhodium when (b) is a promoter based on a metal selectedfrom the group consisting of titanium, manganese, chromium andmolybdenum, and with the further proviso that, when a compound based ononly

ruthenium or

rhodium or

ruthenium and rhodium or

rhodium and nickel

is selected as component (a), the promoter (b) may, if desired, bedispensed with, whereby the catalyst is obtained by

(I) precipitating precursors of the components (a) to (c) from aqueoussolutions in the presence or absence of carriers yielding a precipitate,then

(II) if desired processing the resulting precipitate to give extrudatesor pellets, then

(III) drying the precipitate or pellets or extrudates at a temperaturefrom 80° to 150° C. yielding a dried product, and

(IV) then calcining the dried product at a temperature from 150° to1000° C. in a gas stream comprising air or nitrogen yielding a calcinedproduct, then

(V) if desired, passivating the surface of the calcined product at from20° to 80° C. by means of an oxygen/nitrogen mixture yielding apassivated product, then

(VI) activating the calcined or passivated product by exposing it to areducing atmosphere for from 2 to 24 hours at from 200° to 500° C.

In yet another embodiment of the invention, the objective stated abovecan be achieved by a process for the preparation of aliphaticalpha,omega-aminonitriles by partial hydrogenation of aliphaticalpha,omega-dinitriles at elevated temperature and superatmosphericpressure in the presence of a solvent and of a catalyst, which comprisesusing a catalyst which

(a) contains iron and

(b) contains from 0.01 to 25% by weight, based on (a), of a promoterbased on a metal selected from the group consisting of palladium,platinum, iridium, osmium, iron, copper, silver, gold, tungsten,rhenium, zinc, cadmium, lead, aluminum, tin, phosphorus, arsenic,antimony, bismuth and rare earth metals, and

(c) from 0 to 5% by weight, based on (a), of a trace component based ona metal selected from the group consisting of an alkali metal and analkaline earth metal, whereby the catalyst has a BET-surface of notsmaller than 5 m² /g and a carbon content of not greater than 0.4% byweight, based on the total amount of catalyst.

Preferred catalysts are those in which the component (a) contains atleast one compound based on a metal selected from the group consistingof nickel, cobalt and iron, in an amount of from 10 to 95% by weight,and ruthenium and/or rhodium in an amount of from 0.1 to 5% by weight,based in each case on the sum of the component (a) to (c),

the component (b) contains at least one promoter based on a metalselected from the group consisting of silver, copper, manganese,rhenium, lead and phosphorus, in an amount of from 0.1 to 5% by weight,based on (a), and

the component (c) contains at least one compound based on the alkalimetals and alkaline earth metals selected from the group consisting oflithium, sodium, potassium, cesium, magnesium and calcium, in an amountof from 0.1 to 5% by weight.

Particularly preferred catalysts are:

catalyst A, containing 90% by weight of cobalt oxide (CoO), 5% by weightof manganese oxide (Mn₂ O₃), 3% by weight of phosphorus pentoxide and 2%by weight of sodium oxide (Na₂ O),

catalyst B, containing 20% by weight of cobalt oxide (CoO), 5% by weightof manganese oxide (Mn₂ O₃), 0.3% by weight of silver oxide (Ag₂ O), 70%by weight of silica (SiO₂), 3.5% by weight of alumina (Al₂ O₃), 0.5% byweight of iron oxide (Fe₂ O₃), 0.5% by weight of magnesium oxide (MgO)and 0.5% by weight of calcium oxide (CaO), and

catalyst C, containing 20% by weight of nickel oxide (NiO), 66.4% byweight of silica (SiO₂), 3.7% by weight of alumina (Al₂ O₃), 0.8% byweight of iron oxide (Fe₂ O₃), 0.76% by weight of magnesium oxide (MgO),1.92% by weight of calcium oxide (CaO), 3.4% by weight of sodium oxide(Na₂ O) and 2.0% by weight of potassium oxide (K₂ O).

The catalysts which can be used according to the invention may beunsupported or supported catalysts. Examples of suitable carriers areporous oxides, such as alumina, silica, aluminosilicates, lanthanumoxide, titanium dioxide, zirconium dioxide, magnesium oxide, zinc oxideand zeolites, as well as active carbon or mixtures thereof.

As a rule, the preparation is carried out by precipitating precursors ofthe component (a) together with precursors of the promoters (components(b) and, if desired, with precursors of the trace components (c) in thepresence or absence of carriers (depending on which catalyst type isdesired), if desired processing the resulting catalyst precursor to giveextrudates or pellets, drying the latter and then calcining them.Supported catalysts are also obtainable in general by impregnating thecarrier with a solution of the components (a), (b) and, if desired, (c),where the individual components may be added simultaneously or insuccession, or by spraying the components (a), (b) and, if desired, (c)onto the carrier by a method known per se.

Suitable precursors of the components (a) are as a rule readilywater-soluble salts of the abovementioned metals, such as nitrates,chlorides, acetates, formates and sulfates, preferably nitrates.

Suitable precursors of the components (b) are as a rule readilywater-soluble salts or complex salts of the abovementioned metals, suchas nitrates, chlorides, acetates, formates and sulfates and inparticular hexachloroplatinate, preferably nitrates andhexachloroplatinate.

Suitable precursors of the components (c) are as a rule readilywater-soluble salts of the abovementioned alkali metals and alkalineearth metals, such as hydroxides, carbonates, nitrates, chlorides,acetates, formates and sulfates, preferably hydroxides and carbonates.

The precipitation is carried out in general from aqueous solutions,either by adding precipitating reagents or by changing the pH or thetemperature.

The preliminary catalyst material thus obtained is usually dried, ingeneral at from 80° to 150° C., preferably from 80° to 120° C.

Calcining is usually carried out at from 150° to 1000° C., preferablyfrom 200° to 450° C., in a gas stream comprising air or nitrogen.

After the calcination, the catalyst material obtained is generallyexposed to a reducing atmosphere (activation), for example to a hydrogenatmosphere or a gas mixture containing hydrogen and an inert gas, suchas nitrogen, for from 2 to 24 hours at from 80° to 250° C., preferablyfrom 80° to 180° C., in the case of catalysts based on ruthenium orrhodium as component (a) or from 200° to 500° C., preferably from 250 to400° C., in the case of catalysts based on a metal selected from thegroup consisting of nickel, cobalt and iron as component (a). Thecatalyst space velocity here is preferably 200 l per l of catalyst.

The activation of the catalyst is advantageously carried out directly inthe synthesis reactor, since this usually dispenses with an otherwisenecessary intermediate step, ie. the passivation of the surface at,usually, from 20° to 80° C., preferably from 25° to 35° C., by means ofan oxygen/nitrogen mixture, such as air. The activation of passivatedcatalysts is then preferably effected in the synthesis reactor at from180° to 500° C., preferably from 200° to 350° C., in ahydrogen-containing atmosphere.

The catalysts may be used as fixed-bed catalysts by the liquid-phase ortrickle-bed procedure or as suspension catalysts.

The starting materials used in the novel process are aliphaticalpha,omega-dinitriles of the general formula I

    NC--(CH.sub.2).sub.n --CN                                  I

where n is an integer from 1 to 10, in particular 2, 3, 4, 5 or 6.Particularly preferred compounds I are succinonitrile, glutaronitrile,adiponitrile, pimelonitrile and suberonitrile, very particularlypreferably adiponitrile.

In the novel process, the dinitriles I described above are partiallyhydrogenated in the presence of a solvent using a catalyst to givealpha,omega-aminonitriles of the formula II

    NC--(CH.sub.2).sub.n --CH.sub.2 --NH.sub.2                 II

where n has the abovementioned meanings. Particularly preferredaminonitriles II are those in which n is 2, 3, 4, 5 or 6, in particular4, ie. 4-aminobutyronitrile, 5-aminopentanenitrile, 6-aminohexanenitrile(6-aminocapronitrile), 7-aminoheptanenitrile and 8-aminooctanenitrile,very particularly preferably 6-amino-capronitrile.

If the reaction is carried out in a suspension, temperatures of from 40°to 150° C., preferably from 50° to 100° C., particularly preferably from60° to 90° C., are usually chosen; the pressure is chosen in general tobe from 2 to 20, preferably from 3 to 10, particularly preferably from 4to 9, MPa. The residence times are essentially dependent on the desiredyield and selectivity and on the desired conversion; usually, theresidence time is chosen so that a maximum yield is obtained, forexample from 50 to 275, preferably from 70 to 200, minutes whenadiponitrile is used.

In the suspension procedure, preferably used solvents are ammonia,amines, diamines and triamines of 1 to 6 carbon atoms, such astrimethylamine, triethylamine, tripropylamine and tributylamine, oralcohols, in particular methanol and ethanol, particularly preferablyammonia. A dinitrile concentration of from 10 to 90, preferably from 30to 80, particularly preferably from 40 to 70, % by weight, based on thesum of dinitrile and solvent, is advantageously chosen.

The amount of catalyst is chosen in general so that the amount ofcatalyst is from 1 to 50, preferably from 5 to 20, % by weight, based onthe amount of dinitrile used.

The suspension hydrogenation can be carried out batchwise or,preferably, continuously, as a rule in the liquid phase.

The partial hydrogenation can also be carried out batchwise orcontinuously in a fixed-bed reactor by the trickle-bed or liquid-phaseprocedure, a temperature of from 20° to 150° C., preferably from 30° to90° C., and a pressure of, as a rule, from 2 to 30, preferably from 3 to20, MPa generally being chosen. According to the invention, the partialhydrogenation is carried out in the presence of a solvent, preferablyammonia, amines, diamines and triamines of 1 to 6 carbon atoms, such astrimethylamine, triethylamine, propylamine and tributylamine, oralcohols, preferably methanol and ethanol, particularly preferablyammonia. In a preferred embodiment, an ammonia content of from 1 to 10,preferably from 2 to 6, g per g of adiponitrile is chosen. A catalystspace velocity of from 0.1 to 2.0, preferably from 0.3 to 1.0, kg ofadiponitrile per l per h is chosen. The conversion and hence theselectivity can be controlled by changing the residence time in thiscase too.

In the novel process, alpha,omega-aminonitriles are obtained in goodselectivities and with only small amounts of hexamethylenediamine.Furthermore, the catalysts used according to the invention have asubstantially longer life than comparable prior art catalysts. Thealpha,omega-aminonitriles are important starting compounds for thepreparation of cyclic lactams, in particular 6-aminocapronitrile forcaprolactam.

EXAMPLES Comparative Example 1 (Example 2 in DE-A 848,654)

A tube reactor having a length of 4.5m and an internal diameter of 0.6cm was filled with 105 ml (96 g) of catalyst consisting of 2.3% byweight of PdO on Sio₂ (remainder), and the catalyst was then activatedat atmospheric pressure in the course of 48 hours in a stream ofhydrogen (200 l/h) by increasing the temperature from 30° C. to 250° C.After the temperature had been reduced to 120° C. a mixture of 55 ml/hof adiponitrile (AND), 130 ml/h of ammonia and 200 l/h of hydrogen wasfed to the reactor at 180 bar. Under these conditions, 13% of theadiponitrile were converted. The reaction mixture consisted essentiallyof 87% by weight of AND and 3.3% by weight of ACN (6-aminocapronitrile).Under these conditions, the catalyst lost 3% of its initial activity perhour of operation.

Comparative Example 2 (Example 4 in DE-A 848,654)

Using 4% by weight of CuO, 4% by weight of ZnO and 16.6% by weight ofCo₂ O₃ on SiO₂ (remainder) as the catalyst, a mixture of 55 ml/h ofadiponitrile, 130 ml/h of ammonia and 200 l/h of hydrogen was reacted toa conversion of 50% at 80° C. and 180 bar in the same reactor as inComparative Example 1. The reacted mixture consisted of 50% by weight ofAND, 40% by weight of ACN and 9% by weight of HMD(hexamethylenediamine). By increasing the reaction temperature to 95°C., the conversion increased to 69%. The reaction mixture consistedessentially of 31% by weight of AND, 46% by weight of ACN and 21% byweight of HMD. Under these conditions, the catalyst lost 1% of itsinitial activity per hour of operation, and the moldings had completelydisintegrated after 60 hours.

Comparative Example 3 (Example 3 in DE-A 848,654)

Using 7.5% by weight of CoO and 16% by weight of Fe₂ O₃ on SiO₂(remainder) as a catalyst, a mixture of 55 ml/h of adiponitrile, 130ml/h of ammonia and 200 l/h of hydrogen was reacted to a conversion of45% at 70° C. and 180 bar in the same reactor as in ComparativeExample 1. The reacted mixture consisted essentially of 55% by weight ofAND, 37% by weight of ACN and 7% by weight of HMD. By increasing thereaction temperature to 85° C., the conversion increased to 78%. Thereaction mixture consisted essentially of 22% by weight of AND, 48% byweight of ACN and 27% by weight of HMD. The catalyst lost 0.5% of itsinitial activity per hour of operation, and 10% of its initial activityin the course of 24 hours.

Example 1

A tube reactor having a length of 2 m and an internal diameter of 2.5 cmwas filled with 750 ml (1534 g) of catalyst consisting of 90% by weightof CoO, 5% by weight of Mn₂ O₃, 3% by weight of P₂ O₅ and 2% by weightof Na₂ O, and the catalyst was then activated at atmospheric pressure inthe course of 48 hours in a stream of hydrogen (500 l/h) by increasingthe temperature from 30° C. to 280° C. After the temperature had beendecreased to 60° C., a mixture of 400 ml/h of adiponitrile, 930 ml/h ofammonia and 500 l/h of hydrogen was fed to the reactor at 200 bar. Underthese conditions, 46% of adiponitrile were converted. The reactionmixture consisted essentially of 54% by weight of AND, 37% by weight ofACN and 9% by weight of HMD. By increasing the reaction temperature to70° C., the conversion increased to 65%. The reaction mixture consistedessentially of 34.5% by weight of AND, 46% by weight of ACN and 19.5% byweight of HMD. After 900 hours, the catalyst still had the sameselectivity as fresh catalyst, the activity being unchanged. Thecatalyst moldings were still intact after removal (after 900 hours).

Example 2

A tube reactor having a length of 4.5 m and an internal diameter of 0.6cm was filled with 105 ml (96 g) of catalyst consisting of 20% by weightof CoO, 5% by weight of Mn₂ O₃, 0.3% by weight of Ag₂ O, 70% by weightof SiO₂, 3.5% by weight of Al₂ O₃, 0.4% by weight of Fe₂ O₃, 0.4% byweight of MgO and 0.4% by weight of CaO, and the catalyst was thenactivated at atmospheric pressure in the course of 48 hours in a streamof hydrogen (200 l/h) by increasing the temperature from 30° C. to 250°C. After the temperature had been decreased to 90° C., a mixture of 55ml/h of adiponitrile, 130 ml/h of ammonia and 200 l/h of hydrogen wasfed to the reactor at 180 bar. Under these conditions, 30% of theadiponitrile were converted. The reaction mixture consisted essentiallyof 65% by weight of AND, 30% by weight of ACN and 4% by weight of HMD.By increasing the reaction temperature to 100° C., the conversionincreased to 71%. The reaction mixture consisted essentially of 29% byweight of AND, 53% by weight of ACN and 18% by weight of HMD. After 300hours, the catalyst still had the same selectivity as fresh catalyst,the activity being unchanged.

Example 3

A tube reactor having a length of 4.5m and an internal diameter of 0.6cm was filled with 105 ml (96 g) of catalyst consisting of 20.0% byweight of NiO, 67.42% by weight of SiO₂, 3.7% by weight of Al₂ O₃, 0.8%by weight of Fe₂ O₃, 0.76% by weight of MgO, 1.92% by weight of CaO,3.4% by weight of Na₂ O and 2.0% by weight of K₂ O, and the catalyst wasthen activated at atmospheric pressure in the course of 48 hours in astream of hydrogen (200 l/h) by increasing the temperature from 30° C.to 250° C. After the temperature had been decreased to 110° C., amixture of 50 ml/h of adiponitrile, 130 ml/h of ammonia and 200 l/h ofhydrogen was fed to the reactor at 180 bar. Under these conditions, 25%of the adiponitrile were converted. The reaction mixture consistedessentially of 75% by weight of AND, 24% by weight of ACN and 0.5% byweight of HMD. By increasing the reaction temperature to 120° C., theconversion increased to 60%. The reaction mixture consisted essentiallyof 40% by weight of AND, 53% by weight of ACN and 5% of HMD. Thecatalyst had a constant activity over 100 hours.

Example 4

A tube reactor having a length of 2m and an internal diameter of 2.5 cmwas filled with 750 ml (1534 g) of a catalyst consisting of 90% b.w. ofCoO, 5% b.w. of Mn₂ O₃, 3% b.w. of P₂ O₅ and 2% b.w. of Na₂ O, and thecatalyst was then activated at atmospheric pressure in the course of 48hours in a stream of hydrogen (500 l/h) by increasing the temperaturefrom 30° to 280° C. After the temperature had been decreased to 55° C.(entrance), 70° C. (exit) resp., a mixture of 400 ml/h ofadipodinitrile, 1900 ml/h of ammonia and 500 l/h of hydrogen was fed tothe reactor at 200 bar. Under these conditions, 50% of adipodinitrilewere converted. The reaction mixture consisted of essentially of 50%b.w. of AND, 39% b.w. of ACN, and 11% b.w. of HMD (ACN-selectivity: 78%,ACN+HMD-selectivity: 100%). After 3,000 hours the catalyst still had thesame selectivity as fresh catalyst, the activity being unchanged.

Example 5

A catalyst was prepared according to ,,Catalyst Manufacture, A. B.Stiles, T. A. Koch (1995) p. 167-168 by melting iron-oxide (magnetite)with the following promotors: Al₂ O₃, K₂ O as K₂ CO₃, and CaO as CaCO₃.Thereafter, the solidified melt was crushed. The obtained powder had thefollowing composition: 1.1% b.w. K₂ O, 3.0% b.w. Al₂)₃, 2.3% b.w. CaO,remainder FeO/Fe₂ O₃.

After reduction of the above obtained oxidic powder at a temperature of450° C. in a stream of hydrogen (without pressure) during ten hours, thethus treated powder was cooled down to room temperature in a stream ofair and nitrogen. The thus obtained catalyst had a BET-surface of 6.5 m²/g and a carbon content of 0.055%, based on the total amount ofcatalyst.

Three tube reactors in series (total length: 4.5 m, internal diameter0.6 cm) were filled with 115 ml (303 g) of the above obtained catalyst,and the catalyst was then activated at atmospheric pressure in a streamof hydrogen (200 l/h) by increasing the temperature from 50° to 340° C.during the first 24 hours, and then kept at 340° C. during the following72 hours. After the temperature had been decreased to 120° C., a mixtureof 55 ml/h AND, 260 ml/h ammonia and 200 l/h of hydrogen was fed to thereactor at 250 bar.

After a 200 hours the conversion of AND was 47%. The reaction mixtureconsisted essentially of 53% b.w. AND, 38% b.w. ACN and 8% b.w. HMD(ACN-selectivity: 80.9%, ACN+HMD-selectivity: 98%) during the following400 hours.

Example 6

To an aqueous solution of cobalt nitrate, copper nitrate, manganesenitrate and phosphoric acid, consisting of 9.3% b.w. of cobalt, 2.7%b.w. of copper, 0.9% b.w. of manganese and 0.5% b.w. of phosphoric acid,based on the total amount of the solution, a 20% b.w. solution of sodiumcarbonate was added at a temperature of 50° C., yielding thereby aprecipitate. The thus obtained precipitate was washed, until the washwater was free of sodium and nitrate. The washed precipitate was mixedwith water and sprayed at a temperature of 550° C. (temperature at theentrance of a spraying tower).

The sprayed powder was dried at 500° C., and processed to extrudateswith a diameter of 4 mm. The extrudates were dried at a temperature inthe range of 100° to 120° C. and then calcined at 900° C. for 1 h. Then,the calcined extrudates (66% b.w. CoO, 20% b.w. CuO, 7.3% b.w. Mn₃ O₄3.6% b.w. MoO₃, 0.1% b.w. Na₂ O, 3% b.w. H₃ PO₄) were reduced in astream of hydrogen at 320° C., and passivated in a stream of air andnitrogen at room temperature.

53 g of the above obtained passivated catalyst were reduced in a streamof hydrogen (20 l/h) at 200° C. for 10 hours and then filled into anautoclave with a volume of 270 ml. Then, 36 g AND, 54 g (89 ml) ammoniawere added. The following table shows the results of the hydrogenation:

                  TABLE                                                           ______________________________________                                        ex. 6                                                                                 reaction ACN-    HMD-   ACN-   ADN-                                   temp./press.                                                                          time     yield   yield  selectivity                                                                          conversion                              °C./bar!                                                                       h!       %!      %!     %!     %!                                    ______________________________________                                        50/200  5        40      13     76     53                                     50/200  6        44      17     72     61                                     ______________________________________                                    

Example 7

142 g alpha-Al₂ O₃ (Spheralite®512B, Rhone-Poulenc, spheres with adiameter in the range of 3 to 6 mm, water absorption=0,488 ml/g, bulkdensity=800 g/l) was impregnated with 69 ml of a solution of rutheniumnitrate, obtained by diluting 7.21 g of a solution of ruthenium nitratewith a Ru-content of 19.9% b.w. with water to a volume of 69 ml, for 30minutes. Then the impregnated spheres were dried for 16 h at 120° C. andthereafter calcined for 4 h at 300° C., yielding a catalyst with 1% b.w.of Ru, based on the total amount of the catalyst.

Example 8

225 g Al₂ O₃ (D10-12, from BASF, extrudates with a diameter of 4 mm,water absorption=0,44 ml/g, bulk density=879 g/l, BET-surface=95m² /g)was impregnated with 100 ml of a solution of ruthenium nitrate, obtainedby diluting 59.51 g of a solution of ruthenium nitrate with a Ru-contentof 19.9% b.w. with water to a volume of 100 ml, for 120 minutes. Thenthe impregnated extrudates were dried for 16 h at 120° C. and thereaftercalcined for 4 h at 300° C., yielding a catalyst with 5% b.w. Ru, basedon the total amount of the catalyst.

Example 9

90 g Kieselguhr (extrudates with a diameter of 4 mm, waterabsorption=0,77 ml/g, bulk density=504 g/l) was impregnated with 70 mlof a solution of ruthenium nitrate, obtained by diluting 4.57 g of asolution of ruthenium nitrate with a Ru-content of 19.9% b.w. with waterto a volume of 70 ml, for 120 minutes. Then the impregnated extrudateswere dried for 16 h at 120° C. and thereafter calcined for 4 h at 300°C., yielding a catalyst with 1% b.w. of Ru, based on the total amount ofthe catalyst.

Examples 10-12

31 ml catalyst were reduced in a stream of hydrogen (20 l/h) at 200° C.for 10 hours and then filled into an autoclave having a volume of 270ml. Then, 36 g AND and 54 g (89 ml) ammonia were added. The followingtable shows the results.

                  TABLE                                                           ______________________________________                                        ex. 10-12                                                                                    reaction time                                                                             selectivity of                                                                         selectivity of                                            h!         ACN      ACN + HMD                                      temp./press.                                                                            (ADN-conv. =                                                                              (ADN-conv. =                                                                           (ADN-conv. =                              ex.   °C./bar!                                                                        50%)        50%)     50%)                                      ______________________________________                                        7    130/200   2.9         72.4     99.3                                      8     50/200   1.7         80.4     99.1                                      9    110/200   4.3         75.1     99.2                                      ______________________________________                                    

Example 13

The catalyst of example 5 was washed with water for 24 hours at 60° C.,yielding a catalyst with the following composition: 0.08% b.w. K₂ O,3.0% b.w. Al₂ O₃, 2.3% b.w. CaO, remainder FeO/Fe₂ O₃.

After reduction of the above obtained oxidic powder at a temperature of450° C. in a stream of hydrogen (without pressure) during ten hours, thethus treated powder was cooled down to room temperature in a stream ofair and nitrogen. The thus obtained catalyst had a BET-surface of 7 m²/g and a carbon content of 0.05%, based on the total amount of catalyst.

Three tube reactors in series (total length: 4.5 m, internal diameter0.6 cm) were filled with 115 ml (290 g) of the above obtained catalyst,and the catalyst was then activated at atmospheric pressure in a streamof hydrogen (200 l/h) by increasing the temperature from 50° to 340° C.during the first 24 hours, and then kept at 340° C. during the following72 hours. After the temperature had been decreased to 115° C., a mixtureof 55 ml/h AND, 260 ml/h ammonia and 200 l/h of hydrogen was fed to thereactor at 250 bar.

After 50 hours the conversion of AND was 50%. The reaction mixtureconsisted essentially of 50% b.w. AND, 42% b.w. ACN and 7.5% b.w. HMD(ACN-selectivity: 84%, ACN+HMD-selectivity: 99%) during the following100 hours.

Example 14

To an aqueous solution of FeCl₂ a solution of NaOH was added yielding aprecipitate of y-FeOOH, which was subsequently separated by filtrationand dried at 120° C. for 16 hours. The dried powder was reduced at 400°C. in a fixed-bed with hydrogen without pressure to metallic ironpowder. The thus obtained pyrophoric iron powder was passivated in anitrogen/air mixture at 40° C. for 8 hours, yielding a powder with ametallic iron content 93%. The thus passivated iron powder was mixedwith 2% b.w. of graphite, based on the total amount of graphite and ironpowder, and shaped into pellets (5 mm length, 3 mm diameter). The thusobtained catalyst had a BET-surface of 9 m² /g.

31 ml (71 g) catalyst were reduced in a stream of hydrogen (10 l/h,without pressure) at 450° C. for 24 hours and then filled into anautoclave having a volume of 270 ml. Then, 36 g AND and 54 g (89 ml)ammonia were added. The following table shows the results after 5 and6.5 hours.

                  TABLE                                                           ______________________________________                                        ex. 14                                                                                reaction  yield   yield   ACN-  conversion                            temp./press.                                                                          time      (ACN)   (HMD)   select.                                                                             (ADN)                                  °C./bar!                                                                       h!        %!      %!      %!    %!                                   ______________________________________                                        70/200  5         42.5    9       82    52                                    70/200  6.5       52      12      80    65                                    ______________________________________                                    

We claim:
 1. In a process for the preparation of aliphaticalpha,omega-aminonitriles by partial hydrogenation of aliphaticalpha,omega-dinitriles at elevated temperature and superatmosphericpressure in the presence of a solvent and a catalyst, the improvementwhich comprises: carrying out the partial hydrogenation in the presenceof a catalyst which(a) contains a compound based on a metal selectedfrom the group consisting of cobalt, iron, nickel, ruthenium andrhodium, (b) contains from 0.01 to 25% by weight, based on (a), of apromotor based on a metal selected from the group consisting ofpalladium, platinum, iridium, osmium, iron, copper, silver, gold,chromium, molybdenum, tungsten, manganese, rhenium, zinc, cadmium, lead,aluminum, tin, phosphorus, arsenic, antimony, bismuth and rare earthmetals and (c) from 0 to 5% by weight, based on (a), of a tracecomponent based on a metal selected from the group consisting of analkali metal and an alkaline earth metal, with the proviso that thecomponent (a) is not based oniron or iron and one of the metals selectedform the group consisting of cobalt, ruthenium and rhodium when (b) ispromoter based on a metal selected from the group consisting oftitanium, manganese, chromium and molybdenum, and with the furtherproviso that, when a compound based on onlyruthenium or ruthenium andrhodium or rhodium and nickelis selected as component (a), the promoter(b) may, optionally, be dispensed with, whereby the catalyst is obtainedby(I) impregnating a catalyst carrier with a solution of the components(a), (b) and, optionally, (c), where the individual components may beadded simultaneously or in succession, or by spraying the solutions ofthe components (a), (b) and, optionally, (c) onto the carrier, then (II)optionally processing the resulting impregnated carrier to giveextrudates or pellets, then (III) drying the impregnated carrier,extrudates or pellets at a temperature from 80° to 150° C. yielding adried product, and (IV) then calcining the dried product at atemperature from 150 to 1000° C. in a gas stream comprising air ornitrogen yielding a calcined product, then (V) optionally, passivatingthe surface of the calcined product at from 20° to 80° C. by means of anoxygen/nitrogen mixture yielding a passivated product, then (VI)activating the calcined or passivated product by exposing it to areducing atmosphere for from 2 to 24 hours at from 200° to 500° C.